EP0348007B1 - Dispositif de déchargement aéré - Google Patents

Dispositif de déchargement aéré Download PDF

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Publication number
EP0348007B1
EP0348007B1 EP89201645A EP89201645A EP0348007B1 EP 0348007 B1 EP0348007 B1 EP 0348007B1 EP 89201645 A EP89201645 A EP 89201645A EP 89201645 A EP89201645 A EP 89201645A EP 0348007 B1 EP0348007 B1 EP 0348007B1
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EP
European Patent Office
Prior art keywords
plugs
gaseous fluid
jacket
walls
particulate solids
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Expired - Lifetime
Application number
EP89201645A
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German (de)
English (en)
Other versions
EP0348007A1 (fr
Inventor
Hendricus Arien Dirkse
Andrew Michael Scott
Thomas Sean Dewitz
Rene Rombout
Charles Michael Arbore
Uday Mahagaokar
Rudi Everts
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Shell Internationale Research Maatschappij BV
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Shell Internationale Research Maatschappij BV
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Application filed by Shell Internationale Research Maatschappij BV filed Critical Shell Internationale Research Maatschappij BV
Publication of EP0348007A1 publication Critical patent/EP0348007A1/fr
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Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/48—Apparatus; Plants
    • C10J3/50—Fuel charging devices
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/0015—Feeding of the particles in the reactor; Evacuation of the particles out of the reactor
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2200/00—Details of gasification apparatus
    • C10J2200/15—Details of feeding means

Definitions

  • the invention relates to an apparatus for maintaining a uniform mass flow rate of particulate solids and gas mixture discharged from a holding vessel apparatus to a reactor, comprising means for introducing said mixture into a receiving means having converging walls which form at least one port at the apex thereof for discharging said mixture therefrom. More in particular, this invention relates to pulverized coal discharged to a gasifier for the manufacture of synthesis gas.
  • the present invention is directed to overcoming this problem in the art both for uniform flow and for reliable continuous flow.
  • the apparatus of the invention therefore is constructed such that the receiving means comprises an inner shell and a jacket surrounding the inner shell, and mounted to form a substantially enclosed space between the walls of the inner shell and said jacket, said jacket having at east one outlet port at the converging end thereof in axial alignment with the discharge port of said receiving means; and wherein a plurality of plugs is mounted in said walls, said plugs being porous to gaseous fluids and wherein one face of said plugs is exposed to said particulate solids and gas mixture, said jacket being provided with a partition within the substantially enclosed space forming at least two substantially enclosed compartments; means for selectively injecting gaseous fluid under pressure into said compartments; and means for independently controlling the flow rate and direction of said gaseous fluid under pressure at a rate sufficient to fluidize the particulate solids in proximity to said portion of porous plugs but at a rate below that which would fluidize the particulate solids located beyond the wide end of
  • synthesis gas occurs by partially combusting a carbonaceous fuel, such as coal, at relatively high temperatures in the range of 1000 °C-3000 °C and at a pressure range of from about 1-200 bar, in the presence of oxygen or oxygen-containing gases in a coal gasification reactor, hereinafter referred to as a gasifier.
  • a carbonaceous fuel such as coal
  • oxygen or oxygen-containing gases in a coal gasification reactor, hereinafter referred to as a gasifier.
  • Steam, carbon monoxide, carbon dioxide and oxygen-containing gases including air, oxygen-enriched air, and oxygen are optionally diluted with nitrogen and/or other inert gases.
  • the fuel and gas mixture is discharged from a feed vessel apparatus, advantageously having multiple outlets, each outlet being in communication with at least one burner associated with the gasifier.
  • a gasifier will have burners in diametrically opposing positions, but this is not required for this invention.
  • the burners have their discharge ends positioned to introduce the resulting flame and the agent of combustion into the gasifier.
  • the coal mass flow rate should advantageously be constant over periods of this order and advantageously over shorter periods to maintain constant local conditions.
  • the present invention utilizes a vessel having downwardly-converging walls at the lower end thereof forming a portion having plugs of porous material for aerating the solids within the vessel, and having at least one port at the apex so as to maintain a uniform mass flow rate of the solids and gas mixture discharged to a gasifier.
  • areas located circumferentially about the outside of the porous material portion are isolated to form one or more closed compartments. Gaseous fluids are injected into each compartment at selected pressure and rate to maintain a uniform mass flow rate of a particulate solids and gas mixture to be discharged to the receiving gasifier.
  • the interchangeability of porous material portions having different permeabilities provide greater flexibility for operating the process under varying conditions, such as different coal types, coal moisture content, etc. This configuration can be changed depending on the solids flow characteristics and properties.
  • An advantage of the present invention is that maintaining a uniform mass flow rate of a particulate solids and gas mixture to a gasifier prevents the occurrence of zones of underheating and overheating within the gasifier.
  • a further advantage of the present invention is the protection afforded the refractory lining within the gasifier due to the prevention of zones of underheating and overheating.
  • An additional advantage of the present invention is more efficient utilization of fuel in the production of synthesis gas.
  • Another advantage of the present invention is the capability of maintaining high suspension densities, e.g. greater than 50 to 800 kg/m3, in the transport line from the vessel to the gasifier thereby reducing the consumption of aeration and pneumatic transport gas and avoiding dilution of the synthesis gas produced in the gasifier which would make the synthesis gas a less valuable product.
  • the method and apparatus according to the invention are also suitable for reactive solids and other finely divided solid fuels which could be partially combusted, such as lignite, anthracite, bituminous, brown coal, soot, petroleum coke, shale, tar sands, and the like.
  • the size of solid carbonaceous fuel is such that 90 per cent by weight of the fuel has a particle size smaller than 100 mesh (A.S.T.M.).
  • the present invention can be used for both granular, pulverized, and powdered solids such as resins, catalysts, fly ash, and electrostatic precipitator fines, and the like.
  • an apparatus for maintaining a uniform mass flow rate of a particulate solids and gas mixture discharged from a holding vessel apparatus, such as a feed hopper 11 operated at elevated pressures of 1-200 bar, via a conduit 40 to a receiving reactor, such as a gasifier 9, generally includes means for introducing the mixture, such as an inlet port 10, into the feed hopper 11.
  • the feed hopper 11 directs the material into generally cone-shaped receiving means shown generally at 7 and described more particularly with reference to Fig. 2.
  • the receiving means 7 may be lined with a liner or inner shell 8 to be more particularly described with reference to Fig. 3.
  • the liner 8 has converging walls 12 forming an included angle of less than about 150 degrees, in particular less than about 90 degrees, and converging toward at least one port 17 formed at the apex thereof for discharging the mixture therefrom.
  • the receiving means 7 comprises a jacket 13 which surrounds the liner 8 and is mounted to form a substantially enclosed space, or manifold, between the walls 12 of the liner 8 and the jacket 13.
  • the jacket 13 has at least one outlet port 15 at the lower end thereof which is in axial alignment with the discharge port 17 of the liner 8 for discharging particles therefrom.
  • Means for isolating areas advantageously first and second areas 18, 19, respectively, located outside and circumferentially about substantially adjacent portions of porous plugs 14 of walls 12, such as a partition 22 within the substantially enclosed space between the jacket 13 and the walls 12, forms at least two substantially enclosed compartments.
  • the jacket 13 includes means for selectively injecting gaseous fluid under pressure into first and second areas 18, 19, respectively, such as inlet ports 23A, 23B, and 24A, 24B, respectively, from pressurized fluid sources 20, 21, respectively.
  • sources 20, 21 are shown as separate sources, it is recognized by those skilled in the art that gaseous fluid may be supplied from the same source.
  • the compartments formed within the substantially enclosed space between the walls 12 and the jacket 13 permit gaseous fluids, possibly having different densities, such as nitrogen or other inert gas and synthesis gas which is mainly carbon monoxide, hydrogen, and water, to be selectively injected into the compartments.
  • the gas injected from source 20 into the first area 18 may be more, equal, or less dense than the gas injected from source 21 into second area 19.
  • the gas injected into area 18 would be inert and the gas injected into area 19 would be particulate-free synthesis gas.
  • the gas injected into area 18 would flow upwards and could be vented to control the pressure in the feed hopper 11 whereas the gas injected into the area 19 flows downward and is transported to the gasifier 9.
  • the liner 8 is advantageously made of a heavy, solid material such as stainless steel or alloy 20 and contains a plurality of holes such as 32 in the walls 12.
  • the holes 32 are countersunk to receive and retain plugs shown generally at 14 of Figs. 2, 3A and 3B.
  • the plugs 14 are comprised of inserts 16 made of porous material which may be metallic or non-metallic, such as sintered powdered metal, woven stainless steel, or porous ceramic, depending upon the operating conditions and type of coal used in the process.
  • the arrow A in Figs. 3A and 3B represents gas flow. Inserts 16 are held in place by means of a retainer ring 27 which also allows for differential thermal expansion.
  • the porous material of insert 16 has a selected permeability.
  • the porous material of the insert 16 facilitates the uniform distribution of gaseous fluid injected from pressurized sources 20, 21 into the liner 8 and prevents bridging of the particulate solids discharged from the liner 8 via discharge port 17.
  • the pore size of the porous material and the type of porous material of the insert 16 is based on, among other factors, the type of coal or fuel used and the temperature of operation. To allow greater operating flexibility to use various types of coal requiring differing pore sizes, the liner 8 is advantageously interchangeable with another liner having plugs 14 of a different permeability than the first liner 8.
  • the porous material serves to control the bulk density of the mixture within the liner 8 and the discharge rate of the mixture leaving the hopper 11 via port 17.
  • the configuration of the insert 16 of Fig. 3A presents a smoother surface to the particulate solids whereas the configuration of Fig. 3B is simpler from a manufacturing standpoint.
  • the holes 32 are arranged to provide proper aeration for differing particulate matter and characteristics thereof.
  • the holes 32 of the liner 8 may be arranged in three general zones of openness, 33, 34 and 35, where the zone 33 is 3% open, the zone 34 (bridging zone) is 10% open and the zone 35 is 5% open.
  • the entire liner 8 may have approximately 200 holes 32, the diameter of each being on the order of 140 mm.
  • the size of the plugs, configuration of the plugs and mechanical sealing depend also on the mechanical strength criteria, which are related to operating conditions.
  • the flow rate and direction of the gaseous fluid, advantageously nitrogen and synthesis gas, injected under pressure into the first and second areas 18, 19, respectively, are controlled by using flow controllers 25A, 25B, 26A and 26B, respectively, at a rate sufficient to aerate the particulate solids in proximity to the plugs 14 of walls 12, but at a rate below that which would fluidize the particulate solids located above the plugs 14. It is undesirable to inject the gases at a rate sufficient to fluidize the particles above the inserts 16 as is typically done in conventional systems, because it results in more inert gas diluting the synthesis gas produced in the gasifier 9 and thus yielding a less valuable product.
  • the slip velocity above the aeration cone 8 i.e. the relative superficial velocity between the gas and the coal within the hopper, should be less than 50% of the fluidization velocity and in particular near zero. Also, fluidization of the particles increases fluctuations of the mass flow rate of solids discharged from the coal feed hopper 11.
  • Terminal falling velocity is defined as the velocity at which the drag forces on a solid particle due to the flow of gases upward equals the downward force on the particle due to gravity. If the flow rates of the gases exceed the terminal falling velocity, then the solids will be discharged via the vent 50 rather than the discharge port 17.
  • the flow rates of these gases from sources 20 and 21 are independently controllable which permits the separate control of the amount of gas flowing upward and the amount of gas flowing downward relative to the flow of the coal.
  • the rate of injecting nitrogen in the first area would be approximately 100 kg/hr. Should this rate be exceeded then the suspension density would be less than 450 kg/m3 and the synthesis gas produced in the gasifier 9 would be diluted by the nitrogen from source 20. Additionally, should this rate be somewhat less than the selected rate then the suspension density would be substantially higher than 450 kg/m3. Depending on the material and operating conditions, this situation could lead to less than stable flow.
  • gaseous fluid may be injected in various directions and elevations to control the pressure and velocity profile which exists at the discharge port 17.
  • This selective injection provides for separate control of the mixture density within the feed hopper 11 and the discharge density of the mixture leaving the hopper 11 via the outlet port 15.
  • the discharge port 15 of the hopper 11 is much smaller than conventional technologies for suspension densities of 200-500 kg/m3 preferred in the present invention.
  • the diameter of the discharge port 17 in the present invention is about 4 mm to about 150 mm for a solids and gas mixture having a suspension density of about 200-500 kg/m3. This diameter is larger than the maximum bridging diameter of the aerated particulate solids to prevent bridging of the solids as they exit the discharge port 17.
  • Conventional coal feed systems using gravity flow of solids assisted by aeration to break up bridging typically have a suspension density of less than 200 kg/m3 at the discharge outlet of the feed hopper and a corresponding feed vessel apparatus discharge port diameter of greater than about 150 mm.
  • Diameters of the discharge port 17 greater than about 150 mm for a given mass flow rate used in the present invention are not desirable because either the velocity or suspension density would fall below the desired limits thus resulting in fluctuations of the mass flow rate of the coal and gas mixture to the gasifier 9.
  • the smaller discharge port 17 diameter of the present invention in conjunction with the compartmented injection of gaseous fluids, acts like a fluidic valve to control the particulate discharge rate and thereby eliminates the need for troublesome valves in transport hardware between the discharge of the hopper 11 and the gasifier 9.
  • the present invention may be provided with means for venting gas from the upper end of the hopper 11, say via port 50, for the purpose of maintaining an upward flow of gas through the solids in the feed hopper 11 of approximately 2 mm/sec and thereby eliminate local bridging of the solids and provide smoother flow to the discharge port 17.
  • the present invention may incorporate liners 8A and 8B located inside the feed hopper 11, rather than at the lower end of the hopper 11, as shown in Figs. 4 and 5, respectively.
  • An advantage to the embodiment shown in Fig. 4 is that the transport line 40 from the feed hopper 11 to the gasifier 9 would be shorter for plant configurations in which the burners of the gasifier are elevated with respect to the feed hopper. A shorter transport line 40 provides more uniform flow of the coal to the burners of the gasifier 9.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
  • Nozzles (AREA)
  • Solid Fuels And Fuel-Associated Substances (AREA)

Claims (2)

  1. Un dispositif pour maintenir un débit massique uniforme d'un mélange de particules solides et de gaz déchargé d'un appareil à réservoir de retenue (11) dans un réacteur (9), comprenant :
       des moyens pour introduire le mélange dans un moyen de réception (7) ayant des parois convergentes (12) qui forment au moins un orifice (17) à leur sommet pour déchargement du mélange ; le moyen de réception (7) comprenant une enveloppe intérieure (8) au moins partiellement poreuse et une chemise (13) entourant l'enveloppe intérieure (8) et montée de manière à former un espace substantiellement clos entre les parois (12) de l'enveloppe intérieure (8) et la chemise (13), cette chemise ayant au moins un orifice de sortie (15) à son extrémité convergente en alignement axial avec l'orifice de sortie (17) du moyen de réception (7) ; la chemise étant pourvue aussi d'une cloison à l'intérieur de l'espace substantiellement clos formant au moins deux compartiments substantiellement clos ; des moyens (20, 21) pour injecter sélectivement un fluide gazeux sous pression dans les compartiments ; caractérisé par une multiplicité de bouchons (14) montés dans les parois (12), ces bouchons (14) étant poreux pour les fluides gazeux et une face des bouchons étant exposée au mélange de particules solides et de gaz et des moyens (25A, 25B, 26A, 26B) pour régler indépendamment le débit et la direction du fluide gazeux sous pression à un débit suffisant pour fluidiser les particules solides à proximité de ladite portion des bouchons poreux, mais à un débit inférieur à celui qui fluidiserait les particules solides situées au-delà de l'extrémité large des parois convergentes (12), ces moyens comprenant des moyens pour injecter un premier fluide gazeux ayant une masse volumique choisie dans un premier compartiment ; et des moyens pour injecter un second fluide gazeux ayant une masse volumique inférieure à celle du premier fluide gazeux dans un second compartiment.
  2. Le dispositif selon la revendication 1, caractérisé en ce que les bouchons (14) sont disposés dans des zones (33, 34, 35) de pénétrabilité différente de l'enveloppe intérieure (8).
EP89201645A 1988-06-21 1989-06-21 Dispositif de déchargement aéré Expired - Lifetime EP0348007B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US07/209,602 US5106240A (en) 1988-06-21 1988-06-21 Aerated discharge device
US209602 1988-06-21

Publications (2)

Publication Number Publication Date
EP0348007A1 EP0348007A1 (fr) 1989-12-27
EP0348007B1 true EP0348007B1 (fr) 1992-08-26

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EP89201645A Expired - Lifetime EP0348007B1 (fr) 1988-06-21 1989-06-21 Dispositif de déchargement aéré

Country Status (8)

Country Link
US (1) US5106240A (fr)
EP (1) EP0348007B1 (fr)
JP (1) JP2632216B2 (fr)
CN (1) CN1022926C (fr)
AU (1) AU616767B2 (fr)
CA (1) CA1330814C (fr)
DE (1) DE68902593T2 (fr)
ZA (1) ZA894640B (fr)

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Also Published As

Publication number Publication date
DE68902593D1 (de) 1992-10-01
JP2632216B2 (ja) 1997-07-23
CN1022926C (zh) 1993-12-01
AU3657189A (en) 1990-01-04
JPH0245594A (ja) 1990-02-15
US5106240A (en) 1992-04-21
DE68902593T2 (de) 1993-01-21
ZA894640B (en) 1990-02-28
AU616767B2 (en) 1991-11-07
CN1040048A (zh) 1990-02-28
CA1330814C (fr) 1994-07-19
EP0348007A1 (fr) 1989-12-27

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